Regeneration of catalyst for hydrogenation of sugars

ABSTRACT

A process for regenerating catalysts that have been deactivated or poisoned during hydrogenation of biomass, sugars and polysaccharides is described, in which polymerized species that have agglomerated to catalyst surfaces can be removed by means of washing the catalyst with hot water at subcritical temperatures. A feature of the process regenerates the catalysts in situ, which allows the process to be adapted for used in continuous throughput reactor systems. Also described is a continuous hydrogenation process that incorporated the present regeneration process.

BENEFIT OF PRIORITY

The present application claims benefit of priority of InternationalApplication No. PCT/US13/36901, filed Apr. 17, 2013, which claimspriority to U.S. provisional application Ser. No. 61/651,021, filed May24, 2012, of which the entire contents of each are incorporated hereinby reference.

FIELD OF INVENTION

The present invention relates to a process for regenerating catalyststhat have been deactivated or poisoned during hydrogenation of biomassor biomass derivatives. In particular, the invention describes aregeneration process that can bring back catalyst activity inhydrogenation reactors of sugars or polysaccharides, and an associatedreactor system.

BACKGROUND

In recent years, interest in developing renewable and “green” resourcesfor chemical and fuel products has gained considerable momentum. In thisrespect, the exploitation of biomass or bio-based materials (i.e.materials whose carbon content is derived from regenerative biologicalrather than non-regenerative sources) for generating chemical and fuelproducts, which until now have been predominantly derived fromfossil-origin materials, such as petroleum or coal, has become a focusof research and developmental investment. Certain chemical and fuelproduct replacements or alternatives have been produced on a commercialscale from biomass. For example, in the area of liquid fuels, ethanoland biodiesel (i.e. fatty acid alkyl esters) have been produced on acommodity scale from corn and sugar cane (for ethanol) and from variousvegetable oils and animal fats. Even for these examples, though, biomassutilization processes can be improved.

Common raw materials derived from the processing of biomass arecarbohydrates or sugars, which can be treated chemically to modify thecarbohydrates into other useful chemicals. Thermal treatments provide amethod to transform complex biomass, such as forest and agriculturalresidues into liquid oils. In a hydrothermal liquefaction (HTL) process,conversion of carbohydrates is done with wet biomass at elevatedtemperatures (e.g., 300°-350° C., 570°-660° F.). Steam generated byheating the wet biomass results in high pressures (e.g. 15-20 MPa.2,200-3,000 psi). Typically, the conversion is processed in a matter ofminutes (e.g. 5-20 minutes).

Another such chemical treatment process is to hydrogenate carbohydratesinto polyhydric alcohols, which in turn can themselves be furtherprocesses into other useful materials or biofuels. Sugar alcohols, suchas xylitol, sorbitol, and lactitol, are industrially most commonlyprepared by catalytic hydrogenation of corresponding sugar aldehydesover sponge-metal catalysts, such as nickel and ruthenium on carboncatalysts.

Coking and catalyst deactivation is a problem that arises from thehydrogenation of sugar alcohols because of the presence of residualsugars and high molecular weight polymers that have a degree ofpolymerization (DP) number greater than 3 in sugar alcohol solutions.

In many cases process designs, costs and operation schedules are greatlyaffected by the presence of catalyst poisons. Presence of oxidizingagents or small amounts of deactivators can cause either deactivation orpoisoning of the hydrogenation catalyst. Sometimes the reaction product,reaction intermediates or by products act as catalytic deactivators anddo not allow completion of the primary reaction.

In large scale sugar hydrogenation, catalyst deactivation often plays acentral role in the economic efficiency of the hydrogenation process,such as life cycle assessment (LCA). Deactivation of the catalyst can bea complex phenomenon because active sites on catalyst may be blocked bybulky molecules through physical absorption, or poisoned by impurity inthe feed stream, or absorbance of reactants, intermediates and products.Among of the latter, catalyst poisoning by impurities, such as sulfurcompounds, is a key factor for catalyst deactivation. Although, ingeneral, the amount of sulfur contained in biomass is relatively small,however, at large volumes and over time even minimal amounts can buildup and adversely affect catalyst activity. Some biomass can contain asmuch as 0.5 wt. % sulfur. This poisoning impurity has strong interactionwith catalyst surface and can be irreversible.

In a particular situation, one of the problems encountered in thecatalytic hydrogenation of aldose sugars is the deactivation andinstability of the hydrogenation catalyst, for example due to theformation of harmful by-products, such as epimers, hydrolysis productsand their reduction products. Aldonic acids, such as lactobionic acidand xylonic acid, represent one example of the harmful by-productsformed in the hydrogenation of aldoses to alditols. In the hydrogenationof glucose, it has been found that gluconic acid is typically formed asa by-product. It has also been found that gluconic acid has a tendencyto adhere to the catalyst surface thus occupying the active sites of thehydrogenation catalyst and deactivating the catalyst. The deactivationand instability of the catalyst also lead into problems in the recoveryand regeneration of the catalyst. These problems are even more severeespecially with recycled catalysts. Recovery of the catalyst byfiltration can be difficult.

In view of the foregoing, care should be taken to minimize presence ofcatalytic deactivators and poisons in the reaction mixture so as toprolong life of the catalyst. Under such situations some may either optto use a different type of catalyst or seek to clean or regenerate thecatalyst.

Regeneration of deactivated catalysts is possible for many catalyticprocesses and is widely practiced. The main purpose is to remove thetemporary poisons on the catalyst surface and restore the freeadsorption sites. Generally regeneration processes can be categorizedinto two types. i.e. off-site and on-site regeneration. In the off-site(ex-situ) regeneration, the catalyst is unloaded from the reactor andregeneration is performed in moving-bed belt calciners or conical-shapedrotating drum calciners (See. Robinson. D. W., Catalyst Regeneration,Metal Catalysts. Kirk-Othmner Encyclopedia of Chemical Technology[online], 4 Dec. 2000). The on-site (in-situ) regeneration does notrequire removing the catalyst from a reactor. Commonly, the procedure isto burn off, or oxygenate, the temporary poisons, such as green oil, inorder to resume catalyst activity. Regeneration of the catalyst may beaccomplished, for example, by heating the catalyst in air to atemperature over 300° C., up to about 5000° C. to incinerate any organicmaterial, polymers, or char. Catalyst regeneration using suchtechniques, however, has certain limits; one is that repeatedregeneration operations can cause permanent degradation of the catalystactivity.

Another approach is using hot-compressed water as alternatives toorganic solvents and as a medium for unique and/or green chemistry toextract a variety of organic compounds has grown over the recent decade.(Adam G. Carr et al. A Review of Subcritical Water as a Solvent and ItsUtilization for Processing of Hydrophobic Organic Compounds. C HEMICALENGINEERING JOURNAL, v. 172 (2011), pp. 1-17, contents of which areincorporated herein by reference. See also, e.g., M. Osada et al. ENERGY& FUELS 2008, 22, 845-849, contents incorporated herein by reference,pertaining to regenerate catalysts poisoned by sulfur.) Of particularinterest are processes in water near its critical point (T_(c)=374° C.,P_(c)=221 bar (˜3205.33 psi), and p_(c)=0.314 g/ml). Although some haveexplored the use of subcritical water as a solvent and its utility forhydrophobic organic compounds different kinds of reaction materials andcatalytic substrates bring their own associated and distinguishableissues. The reversal of the solvent characteristics of criticalhot-compressed water also results in precipitation of salts that arenormally soluble in room temperature water. Most inorganic salts becomesparingly soluble in supercritical water. This is the basis for uniqueseparation of ionic species in supercritical water. The precipitatedsalts can serve as heterogeneous catalysts for reactions insupercritical water.

In view of the various problems and limitations current regenerativetechniques, a better process for regenerating catalysts used in sugarhydrogenation would be appreciated.

SUMMARY OF THE INVENTION

The present invention describes, in part, a method of reducing catalyticcoking or contamination from sugars or sugar alcohol hydrogenation. Themethod includes: applying a deionized aqueous rinse to a skeletalcatalyst or sponge-metal catalyst at a subcritical temperature whencatalytic activity of the catalysts decreases to a predetermined level.

Alternatively, the invention describes a method of regeneratinghydrogenation catalyst activity in-situ for hydrothermal processing ofsugars or polysaccharides. In particular, the method involves: a)providing a continuous feed hydrogenation reactor containing a catalyst,said reactor being configured to have a first and a second vessel, eachvessel respectively having a first catalyst and a second catalyst, thecatalysts being either the same or of a different material: and b)rinsing each respective vessel and catalyst with subcritical deionizedwater of between about 130° C.-250° C. for an extended period.

Depending on the catalyst material, the method further involves:introducing a subcritical deionized aqueous solution containing H₂O₂ ina concentration of ≦7% by volume to a first catalyst in said firstvessel of said reactor for a period of up to 18 hours when catalyticactivity of said first catalysts decreases to a predetermined level;introducing an aqueous salt solution to a second catalyst in said secondvessel of said reactor for a period of up to 16 hours when catalyticactivity of said second catalyst decreases to a predetermined level;removing said aqueous H₂O₂ solution and said aqueous salt solutionrespectively from said first and second vessels of said reactor; andrinsing each vessel and respective catalyst with subcritical deionizedwater of between about 130° C.-225° C. for a period of at least 4 hours.

The aqueous H₂O₂ solution is applied to the catalyst in the first vesselonce (1) for every single applications of aqueous salt solution atmaximum, or more typically every two or three to eight (2-8)applications of aqueous salt solution applied to the second catalyst inthe second vessel, or as catalytic performance needs may dictate.

In another aspect, the present invention also pertains to a continuoushydrogenation process, which involves a hydrogenation reactor systemwith an in-take port and an extraction port, each of which is connectedin-line to an in-bound channel and an out-bound channel, respectively.Introduce a carbohydrate or sugar solution feedstock and hydrogen into areactor having a catalyst therein. React the feedstock under pressure:remove the resulting aqueous reaction product mixture; and periodicallyintroduce a subcritical deionized water rinse into said first reactorwhen catalytic activity of said catalyst decreases to a predeterminedlevel. The reactor and catalyst are rinsed with subcritical deionizedwater at a temperature between about 130° C., or 135° C.-220° C. or 250°C. for a period of between about 4-24 hours. The reactor system isconfigured as with a first reactor section and second reactor section,each involving a different kind of catalyst material, such that a firstpart reaction involves a first catalyst material and a second partreaction involves a second catalyst material. The first and secondreactor sections are arranged in series relative to each other.

Alternatively, each of the first and second reactors has a first reactorchamber and at least a parallel second reactor chamber. The firstreactor chamber is used alternatively with the parallel second reactorchamber, such that a reactor chamber is washable with the subcriticaldeionized water rinse at a given time, without interruption of saidhydrogenation process. Additionally, one can introduce a deionizedaqueous solution containing H₂O₂ in a concentration of ≦6% or 7% byvolume to the first catalyst in the first reactor for a period of up toabout 18-20 hours when catalytic activity of that first catalystdecreases to a predetermined level. Alternatively, one can rinse with anaqueous 1% to 10% concentration salt solution at a temperature betweenabout 60° C. to about 105° C. over a period of about 6-22 hrs.

The two washing cycles are separate and distinct from each other, hencethey can be performed independently of each other. That is the firstwash does not necessarily influence catalyst regeneration in the secondreactor chamber.

Additional features and advantages of the present methods will bedisclosed in the following detailed description. It is understood thatboth the foregoing summary and the following detailed description andexamples are merely representative of the invention, and are intended toprovide an overview for understanding the invention as claimed.

BRIEF DESCRIPTION OF FIGURES

FIG. 1 is a graph showing an increase of sulfur concentration over timein a skeletal catalyst or sponge-metal catalyst, such as a Raney nickel,fixed-bed reactor, which illustrates a problematic condition that leadsto catalyst poisoning and deactivation.

FIG. 2 is a flow chart showing a schematic representation of a processfor hydrothermal liquefaction of biomass and hydrogenation/hydrolysis ofsugars, and then regenerating the catalysts in situ according to anembodiment of the present inventive process.

FIG. 3 is a schematic representation of an embodiment of ahydrogenation/hydrolysis system according an embodiment of to thepresent invention, in which parallel sets of reactors are used inseries.

FIG. 4 is a graph showing efficiency of reducing the build-up of sulfurconcentration on sponge-metal (e.g., Raney nickel) catalyst afterregenerative washes according to the present invention.

FIG. 5 is a graph showing relative efficiency of sponge-mental (e.g.,Raney nickel) catalyst at converting sugar after regenerative washesaccording to the present invention.

FIG. 6 is a graph showing relative efficiency of sugar conversation withsponge-metal (e.g., Raney nickel) catalyst after regenerative washesaccording to the present invention.

FIG. 7 is a graph showing a reduction in the concentration of sugar(ppm) remaining in a final product over an extended period of running ahydrogenation reaction after regenerative treatment according to aniteration of the present invention.

DETAILED DESCRIPTION OF THE INVENTION Section I Definition of Terms

Before describing the present invention in detail, certain terms thathave meanings generally understood by those of ordinary skill in the artare nevertheless defined herein to better distinguish nuances in meaningthat may apply to different embodiments of the invention. It isunderstood that the definitions provided herein are intended toencompass the ordinary meaning understood in the art without limitation,unless such a meaning would be incompatible with the definitionsprovided herein, in which case the definitions provided control. Thepresent invention is not necessarily limited to specific compositions,materials, designs or equipment, as such may vary. As used in thisspecification and the appended claims, the singular forms “a,” “an,” and“the” include plural referents unless the context clearly dictatesotherwise.

The term “carbohydrate” as used in the specification and claims includesmonosaccharides and polysaccharides. This term includes both purecompounds, such as glucose and sucrose, and mixtures such as cornstarchhydrolyzate, which is a hydrolysis product of cornstarch containingglucose (dextrose) and oligomers thereof.

The term “polysaccharide” as used in the specification and claimsincludes those saccharides containing more than one monosaccharide unit.This term encompasses disaccharides and other saccharides containing asmall number of monosaccharide units, which are commonly known asoligosaccharides.

The term “catalyst poisoning” as used herein refers to an irreversibleadsorption on or reaction with the active surface of a catalyst byreaction product species or impurities (e.g., hydrogen sulfide,cysteine, methionine.)

The term “conversion” as used herein refers to hydrogenation whenapplied to monosaccharides and to a combination of hydrogenation andhydrolysis when applied to polysaccharides.

The term “fouling” as used herein refers to the formation of coke oncatalyst surfaces that block the active sites of the catalyst. Sugaralcohols or polymerized species can undergo dehydration or proteinsundergo denaturation to form polymers that obstruct catalyst surfaces.

The term “subcritical water” as used herein refers to an intermediatestate of water above its boiling point at ambient pressure (>100° C., at0.1 MPa) and below its critical point (≧374° C. at ≧22.1 MPa). Forinstance, temperature and pressure windows like 150<T<370° C. at0.4<p<22 MPa. 300≦T≦350° C. at 10≦p≦18 MPa and 250° C.≦T≦450° C. atp>p_(critical) have been reported. Sometimes other terminology, such as“hot compressed water” (HCW), has been employed generally to refer towater at temperatures above 150° C. and various pressures, or“high-temperature water” (HTW), defined broadly as liquid water above200° C. The term is used to distinguish processes that are performedbelow the critical point, but above the boiling point from reactions insupercritical water. Subcritical water has a controlled temperature andpressure in a range less than that of the critical point according tothe requirement of application. Subcritical water can be used as aninexpensive, non-toxic, non-flammable, clean solvent in organic chemicalresearch and commercial applications.

Section II Description

Conversion of sugars, such as dextrose, pentose, or glucose to sorbitoland xylose to xylitol, by pressure hydrogenation/hydrogenolysis has useda sponge-metal catalyst. A problem that arises frequently is thepoisoning of the catalyst and consequent reduction of catalytic functionover time. The life of hydrogenation catalysts typically lasts onaverage between about 70-95 hours (usually about 80-85 hours) beforeexperiencing a significant loss of active functionality. This poisoningoften results from agglomeration of oligomers and sulfur compounds tothe catalyst surface, which reduces active surface area.

For instance, as in FIG. 1, the concentration of organic orbiological-derived sulfur from a feedstock increases with time. Sulfuris absorbed on catalyst surfaces until the absorption capacity reachesmaximum. After about 700-800 hours of use, the amount of sulfur, whichagglomerates to sponge-metal (e.g., Raney nickel) catalysts in afixed-bed reactor, increases steeply. A typical fresh Raney nickelcatalyst possesses on average an active surface area of about 42 m² pergram. After reacting, the active surface area of the catalyst is reducedon average to about 21 m² per gram, which is almost a 50% reduction.Chemi-absorption analysis shows that the deactivation mechanism appearsto involve polymer materials covering the catalytic surface and sulfurcompounds binding with the nickel. As more sulfur and oligomersagglomerate on catalyst surface, the overall ability of the catalyst toreduce sugars decreases and the amount of residual sugar increases.

In view of dilliculties and issues with some regenerative techniques, anattribute of the present invention is to provide a catalyst regenerationprocess that can bring back catalyst activity, and thereby increase theefficiency of sugar hydrogenation conversion on the regeneratedcatalyst. Unlike the issues associated with sulfur compounds that onemay encounter when processing hydrocarbons in the petrochemicalindustry, hydrogenation and hydrogenolysis of biologically-derivedsugars and other carbohydrates or oils have presented new and uniquechallenges. Such reactions are performed at temperatures lower than 250°C. typically less than about 230° C., which is far less than and outsidethe operational temperature range employed in petrochemical refining.

The present invention presents one solution to these problems. In part,the present invention is directed to the removal or minimization of theagglomeration and build-up of sulfur as well as organic compounds on thecatalyst surface with deionized subcritical water as a solvent. Thepresent invention provides a solution that enables industrial users incontinuous production processing to regenerate the activity of catalystsubstrates in-situ while the reactor remains “online.”

A

According to an aspect of the present invention, the method ofregenerating hydrogenation catalyst activity in-situ involves: a)providing a continuous feed hydrogenation reactor containing a catalyst,said reactor being configured to have a first and a second vessel, eachvessel containing a catalyst; and b) rinsing each vessel and catalystwith subcritical deionized water of between about 130° C.-250° C. for anextended period (e.g., ˜3-4 hours).

Subcritical water at temperatures below about 120° C., or 125° C. didnot exhibit sufficient effective cleaning ability of catalyst surfaces.Water temperatures between about 125° C. and 130° C. showedcomparatively better cleaning results than those at lower temperatures,but were still not sufficiently satisfactory. Hence, the subcriticaldeionized water should be at a temperature in a range between about 130°C. or 135° C. to about 220° C., or 250° C. including any variation orcombination of ranges therein between. Typically, the water is used at atemperature between about 140° C., or 145° C. to about 215° C. or 218°C. or between about to about 148° C. or 152° C. to about 207° C. or 213°C. Desirable water temperatures may range between about 150° C. or 153°C. to about 210° C. or 212° C.; about 154° C., 15° C. or 160° C. toabout 202° C. 207° C., or 208° C.; about 157° C., 165° C., 168° C., or172° C. to about 190° C., 197° C. 200° C., or 205° C. Although designedto solve a problem experienced also in petrochemical reactions, theoperating temperature range of between about 140° C. and 225° C.employed to regenerate catalyst activity in the present inventiveprocess are much lower and distinct from those temperatures used inconventional catalyst regeneration methods. The use of a lower operatingtemperature and water is cost efficient in terms of both energy andrenewable resources.

Depending on the nature or material used as catalyst in each of thevessels, the method can further include introducing a hydrogen peroxidesolution to wash the catalyst surface and interior of the reactor for aperiod of between 6-18 hours. This peroxide solution may be appliedeither at ambient room temperature or at an elevated, subcriticaltemperature. The hydrogen peroxide solution can be a deionized aqueoussolution containing a concentration of between about 0.01% and aboutless than or equal to ≦7%, typically between about 4% to about 5% orabout 6%, by volume of H₂O₂. According to an embodiment, the aqueoussolution containing H₂O₂ can be applied to the first catalyst in thefirst vessel of the reactor for a period of up to 18 hours whencatalytic activity of the first catalysts decreases to a predeterminedlevel (e.g. ≦40% or 50% of original activity).

Additionally, one can introduce periodically an aqueous salt solution toeither first or second catalysts in the reactor system, after reactingand removing the sugar solution feedstock and before introducing thesubcritical deionized water rinse. In an embodiment, the aqueous saltsolution is applied to the second catalyst in the second vessel of thereactor for a period of up to 16 hours when catalytic activity of saidsecond catalyst decreases to a predetermined level. One then removes theaqueous H₂O₂ solution and the aqueous salt solution respectively fromthe first and second vessels of the reactor. Subsequently, the reactorand catalysts are rinsed with subcritical water of between about 140°C.-250° C. for a period of between about 4-48 hours.

Depending on the particular materials and poisons that have agglomeratedto deactivate the catalyst, the subcritical water rinse can be appliedto the catalyst for a period of between about 4 or 5 hours to about 24or 48 hours or any duration therein between. Typically, the residencetime of the subcritical water is for a period of between about 6 or 8hours to about 25 or 30 hours; more typically, between about 7, 10, or12 hours to about 18, 20, or 25 hours. Desirable rinse dwell times arebetween about 12 or 14 hours to about 16 or 22 hours.

The metal of the first catalyst can be a sponge-matrix metal catalyst orsupported metal catalyst, such as Ni, and of the second catalyst can beeither: Ru, Pt, or Pd, supported on a substrate, such as carbon ortitania. As person familiar with catalysis mechanics, the morphologicalstructure of supporting materials for catalysts can influence thechemical character and efficiency of the catalyzed reaction. Hence, whatmay apply to one species of catalyst and support may not be generalizedeasily to apply to similar catalyst systems. For instance, a system thatuses a carbon-supported ruthenium (Ru/C) catalyst functions differentlythan a titania-supported ruthenium (Ru/TiO₂) catalyst. An appreciationof what may function in one system may not for the other is notconveyed.

The peroxide wash can be up to about 5% concentration, in a rangebetween about 0.5% to about 5%. Typically, the peroxide wash is at aconcentration between about 1% or 1.5% to about 4.5% or 4.8%; or, moretypically between about 2% or 3% to about 3.5% or 4%.

The salt solution has a concentration a range between about 1% to about10% concentrations. Typically, the salt concentration is between about1% or 2% to about 7% or 8%. Preferably, the concentration is betweenabout 3% to about 5% or 6%. The salt solution can be prepared from avariety of salt species, but typically the salts are either monovalentor dibasic salts (e.g. NaCl, KCl, Na₂HPO₄, K₂HPO₄. Na₂SO₄).

According to an embodiment, the catalyst is totally submerged within andallowed to soak in the wash solution, while minor agitation can beapplied in the chamber. Agitation can be applied by either physicalmotion or gas bubbling through. Alternatively, one may apply acontinuous flowing stream of washing solution to rinse over the catalystsurface.

In an alternative embodiment, the catalyst regeneration process mayproceed as follows: after draining the reactor chamber of hydrogenationproduct, flushing the chamber with ambient temperature water, and thenwashing with a concentrated salt solution (e.g., NaCl or K₂HPO₄) at atemperature between 60° C. to 105° C. and over a period of 6-22 hrs. Inother iterations, the salt solution wash is conducted at a temperaturebetween about 60° C. and 85° C. for a period of about 8 hours to about20 hours. Desirably, the substrate is washed with the salt solution atabout 70° C. for about 12 hours. The catalyst is then washed with waterfor another 6 to 12 hours under the same temperature condition.Subsequently, the treated catalyst is washed with subcritical water at170-250° C. for about 6-16 hours.

While the salt solution can be used with, for example, either asupported nickel or ruthenium catalyst or both systems, one can alsointroduce an additional peroxide solution wash, which is used with thenickel catalyst system alone.

After applying a hot water wash and either salt solution or peroxidewash, depending on catalyst material, the degree of polymerization (DP))can be reduced by up to about 80% or 85% relative to a used catalystthat is not treated according to the present regenerative method. Theinventive process results in a more uniform distribution of theregenerated catalyst activity. It is believed that when exposing asponge nickel or Ru/C catalyst, for example, to a salt solution for anextended time period, the solution helps removes impurities from proteinabsorbance, and remaining sulfur impurities are oxidized to eithersulfate or sulfite, which can then be washed away by the subcriticalwater.

Treatment with hot water washing removes reactive organic compounds thatmay agglomerate to the catalyst and reactor surfaces. The catalystexhibits regenerated catalytic activity after washing with thesubcritical deionized water rinse, and a prolonged catalytic activeduration of at least two to three (2×-3×) times longer than that of acatalyst that is not washed with the deionized subcritical water rinse.

Depending on catalyst performance and its retardation from sulfurpoisoning, one can wash the catalysts in the reactor vessels withsubcritical hot water as frequently as practicable and necessary. Ifsignificant retardation of the catalytic activity persists, one can washwith the catalyst in situ with a H₂O₂ solution or a salt solution, or inany order or combination of the three—peroxide, salt solution, andsubcritical water. Of these three fluids, deionized subcritical hotwater is employed most frequently. Usually, the number of times the saltsolution rinse applied will be greater or more numerous than the numberof times the peroxide solution is used. One can wash the first vesselcatalyst with peroxide solution between about 1 to 3 or 4 applicationsfor every 1 to 7 or 8 application of aqueous salt solution is applied tothe first catalyst in the first vessel and the second catalyst in thesecond vessel. For example, the peroxide solution is used withsponge-nickel catalyst, but not with Ru/C catalyst, which is washed withthe salt solution. Depending on the need for regeneration and type ofagglomerated organics on the two different catalyst materials, thefrequency of each kind of wash can be expressed as a ratio of peroxideto salt rinses (e.g., 1:1, 1:1.5, 1:2, 1:3, 1:4, 1:4.5, 1:5, 1:6, 1:7,or 1:8).

An advantage of the present method is that it permits regeneration ofcatalysts under relatively mild conditions by means of a simple processof washing with subcritical water and a salt solution rinse. The processremoves chemi-absorption sulfur compounds from the catalyst surface,which can prolong the active life of the catalyst. This feature can leadto saving in both money and time for the manufacturer that hydrolyzesugars and other biologically-derived polysaccharides.

An unexpected result of the present invention is the relative efficiencythat subcritical hot water has demonstrated in catalyst regeneration.Normally, water at ambient temperature is a poor solvent for sulfurcompounds or organic oligomers, while supercritical water(temperature>374° C. pressure>221 atm) is extremely corrosive. One ofthe attractive features of hot-compressed water is the adjustability ofits properties by varying process temperature and pressure. Specific toits solvent properties, the dielectric constant of water can be adjustedfrom 80 at room temperature (˜20° C.) to 5 at its critical point.Therefore, water can solubilize most nonpolar organic compoundsincluding most hydrocarbons and aromatics starting at 200-250° C.

B

The method described generally above can be adapted for used in acontinuous hydrogenation reactor system, which can reduce catalyticdeactivation. Hence, in another embodiment, the present inventive methodprovides continuous hydrogenation process. The process comprises:providing a hydrogenation reactor system with an in-take port and anextraction port, each of which respectively is connected in-line to anin-bound channel and an out-bound channel; introducing a carbohydrate orsugar solution feedstock and hydrogen into a reactor having a catalysttherein: reacting said feedstock under pressure; removing a resultingaqueous reaction product mixture: and periodically introducing asubcritical deionized water rinse into said first reactor when catalyticactivity of said catalyst decreases to a predetermined level. Thereactor and catalyst are rinsed with subcritical deionized water at atemperature, for example, between about 135° C.-220° C. for a period ofbetween 4-24-48 hours. The reactor system is configured as with a firstreactor section and second reactor section, each involving a differentkind of catalyst material, such that a first part reaction involves afirst catalyst material and a second part reaction involves a secondcatalyst material. The first and second reactor sections are arranged inseries relative to each other. Each of the first and second reactors hasa first reactor chamber and at least a parallel second reactor chamber.The first reactor chamber is used alternatively with said parallelsecond reactor chamber, such that a reactor chamber is washable withsaid subcritical deionized water rinse at a given time, withoutinterruption of said hydrogenation process.

The continuous hydrogenation process may further include: introducing adeionized aqueous solution containing H₂O in a concentration of ≦6% or7% by volume to said first catalyst in said first reactor for a periodof up to 18 hours when catalytic activity of said first catalystdecreases to a predetermined level. Additionally, the process mayinvolve introducing periodically an aqueous salt solution to eitherfirst or said second catalyst in said reactor system, after reacting andremoving said sugar solution feedstock and before introducing saidsubcritical deionized water rinse. The first part reaction removessulfur and/or sulfides from said feedstock, before reacting in thesecond part reaction.

The catalyst exhibits regenerated catalytic activity after washing withsaid subcritical deionized water rinse. The catalyst exhibits aprolonged catalytic active duration of at least 3 times longer than thatof a catalyst that is not washed with subcritical deionized water rinse.

The operational temperatures of the hot water washing typically canrange between about 130° C. to about 250° C. Typically, the operationsare conducted at a temperature between about 135° C. or 140° C. to about220° C. or 225° C. More typically, the temperature range is betweenabout 145° C. or 147° C. to about 212° C. or 215° C. In particularembodiments the temperature is between about 150° C. or 152° C. to about205° C. or 208° C.

FIG. 2 depicts a schematic representation of a hydrogenation processaccording to an embodiment of the present invention. This flow chartshows a feed stock of carbohydrate or sugar alcohols is introduced intoa reactor having a first catalyst (e.g., Raney Ni) on a fixed-bed andreacted at an atmosphere of about 1100-1300 psi (e.g. 1200 psi), at atemperature less than or equal to about 140° C. or 150° C. (e.g. 130°C.), to remove sulfur and other containments. The feed is thendischarged to a second reactor chamber here the material is subject tohydrogenation over a second kind of catalyst (e.g., Ru/C). Either one orboth of the first and second catalysts can be a sponge-metal matrixcatalyst. After a time, when the catalysts start to deactivate andcatalytic activity flags, one regenerates the catalysts in situaccording an embodiment of the present process.

Unlike in conventional sugar hydrogenation processes, in which sodiumsalts, sulfur and leach nickel need to be removed by means of an ionexchange process, an advantageous feature of the present invention isthat we can eliminate the necessity for an ion exchange step in thepresent inventive process. According to an aspect of the presentinvention, we describe a continuous hydrogenation system and processthat can enable catalyst regeneration in situ by means of a hot waterwash. In other words, the regeneration does not require removing thecatalysts from the reactor. Previously, the most common process of insitu regeneration was to oxygenate, or burn-off, the temporary poisonsto resume catalytic activity.

As in typical hydrogenation processes, a feedstock of sugars isintroduced and reacted with (hydrogen in each of the first set ofreactor chambers. However, the present invention involves a two-stageprocessing protocol. The first stage takes crude sugar solutions andreacts in the presence of a sacrificial sponge-metal (e.g., nickel)catalyst. The sponge-metal catalyst helps either to reduce the level ofor remove sulfur contaminant in the feedstock. When a fresh catalyst hasbeen used to an extent that its catalytic activity starts to flag, asdetectable from the efficiency and purity of the reaction products, suchthat the activity of the catalyst decreases to a predetermined level(e.g., ≦50%, ≦60%, ≦70%, or ≦75% of initial activity) at which pointregeneration is needed, one can shut off the feedstock directed to thechamber in which one desires to regenerate the catalyst.

According to feature of the present invention, the process involves ahydrogenation reactor system with an in-take port and an extractionport, each of which respectively is connected in-line to an in-boundchannel and an out-bound channel, introducing a carbohydrate or sugarsolution feedstock and hydrogen into a reactor having a catalysttherein, reacting the feedstock under pressure, removing a resultingaqueous reaction product mixture, and periodically introducing asubcritical deionized water rinse into said first reactor when catalyticactivity of said catalyst decreases to a predetermined level. Thereactor and catalyst are rinsed with subcritical deionized water at atemperature between about 135° C.-220° C. for a period of between 4-24hours.

FIG. 3, shows a schematic representation of a reactor system 10according to the present invention. The system has a first set ofreaction chambers or vessels 12 a, 12 b arranged in parallel.

The reaction chambers each have an inlet port 14 and an extraction orexit port 15. A feedstock source and reagents 2 are introduced into eachchamber through the inlet port 14 by means of connecting several tubesor channels. Reacted products, byproducts and waste 20 are removed fromthe chamber through the exit port 15.

The first set of reaction chambers can be connected to a second set ofreaction chambers or vessels 16 a, 16 b that are also arranged inparallel. In each set of reactors there may be two chambers or moremultiple chambers, depending on the size or scope of operations. Thereactor are interconnected with conduit tubes or channels that areregulated with a number of valves 1, which can direct the flow ofreagents and product to and from each set of reaction chambers. In otherwords, reaction product from each set of reactors can be channeledthrough the associated set of values and conduits/pipes. Depending ofthe operation, reaction products, as well as other fluids, from thefirst set of reactors 12 a, 12 b can be directed into either reactorchamber of the second set of reactors 16 a, 16 b or to other receptaclesor waste 20. Hence the first reactor chamber is used alternatively withthe parallel second reactor chamber, such that a reactor chamber iswashable with the subcritical deionized water rinse at a given time,without interruption of the overall hydrogenation process in otherreactor chambers. Desired reaction product can be collected in acontainer or other holding vessel 18. According to certain embodiments,a sponge-metal nickel catalyst (Ni) is situated within each of the firstset of reaction chambers 12 a, 12 b. Likewise, in certain embodiments, aruthenium on carbon (Ru/C) catalyst is used in each of the second set ofreaction chambers 16 a, 16 b.

The reactor system is configured with a first reactor section and secondreactor section, each involving a different kind of catalyst material(e.g. sponge nickel and Ru/C catalysts), such that a first part reactioninvolves a first catalyst material and a second part reaction involves asecond catalyst material. As envisioned, the first part of the reactorassembly reacts to reduce or remove sulfur and/or sulfides from saidfeedstock, before reacting in a second part reaction. This we believecan help reduced poisoning the second catalyst in the second reactor,and help minimize adsorption of DP oligomers.

In the assembly, the first and second reactor sections are arranged inseries relative to each other. Each of the first and second reactors hasa first reactor chamber and at least a parallel second reactor chamber.The parallel configuration of the system permits one to take a chamberoff-line without significantly impacting the continuous nature of theoverall hydrogenation process in other chambers. Individual first andsecond vessels in each section can be arranged either in serialcommunication or alternatively, in parallel communication with eachother that permits them to be connected to a continuous production line.

This combination of configurations is advantageous. Unlike conventionalindustrial batch-processing approaches in which the reactor chamberneeds to be emptied and/or disassembled, the present invention enablescontinuous “online” regeneration of catalyst. Hence, the invention canimprove the overall efficiency, production volume capacity, and reducecosts associated with hydrogenation of sugars or carbohydrates intopolyhydric alcohols for various useful products. The hydrogenationcatalyst occurs in-situ in the reactor. That is, in contrast to what isconventionally done, one does not need to remove the catalyst from thereactor chamber for regeneration.

According to the present invention, the spent catalyst can beregenerated either after introducing a spent catalyst from a reactorinto a fixed bed regenerator, or in situ in the reactor chamber. Thatis, one can either unload the reactor for the washing, or preferably,the reactor can be washed in a continuous process. According to thelatter, the catalyst can remain in the reactor chamber, which avoids theefforts associated with removing the catalyst and provides savings inboth time and cost. The reactor system is well adopted for the presentprocess, as an advantage of the present process is that one canregenerate the catalyst simultaneously with the sugar hydrogenationreaction. The regeneration process can be operated in the sametemperature and pressure range as the hydrogenation reaction. Thus, onedoes not need to re-adjust conditions in a reactor vessel.

Section III Empiricals

The examples in the present section further illustrate and describe theadvantages and qualities of the present invention. The particularmaterials, dimensions, amounts and other parameters are exemplary, andare not intended to necessarily limit the scope of the invention.Hydrogenation of aqueous sugar solutions can be performed in batch andcontinuous reactors using supported nickel and ruthenium catalysts. Ingeneral the present invention can be applied to various “skeletalcatalyst” or sponge-metal catalysts that have physical and chemicalproperties similar to those of Raney nickel. Preparation methods wereprecipitation, impregnation, sol-gel and template syntheses, and SiOC₂.TiO₂, Al₂O₃ and carbon were used as support materials. In the particularexamples discussed herein, we refer to Raney nickel catalysts andruthenium on carbon catalysts (Ru/C).

A

Table 1 is a comparative summary showing the effect of various differentregenerative treatments used to recover catalytic activity of asponge-metal (i.e. Raney nickel) fixed-bed catalyst. A sugar feedstockwith a dry solids (DS) content of about 30%, up to about 40%, issubjected to hydrogenation in the comparative examples. A wash withbleach for about 12 hours showed no regenerative effect at all. Heattreatment at 70° C. and no hydrogen for about 14 hours regenerates lessthan 10% of the catalyst activity. Washing the catalyst with hot waterunder about 1200 psi H₂ for about 4 hours at 200° C., regenerated about80% activity. A 5% peroxide (H₂O₂) wash for about 24 hours appeared tohave the best effect, restoring about 90-95% of catalytic activity.

TABLE 1 Comparison of Methods for Regeneration of Raney Ni-CatalystLiquid Hourly H₂ Catalyst Activity Space Velocity Treatment PressureRecovery (%) (LHSV) Time (hr.) 70° C. wash No <10% 1 14-24 hr.  Bleachwash No 0% 1 6-12 hr. 170° C. 1200 psi 80% 1 4-10 hr. wash H₂O₂ wash No90-95% 1 6-24 hr. Feedstock: 30% DS, 10% DP, 7 ppm of sulfur. ReactionCatalyst reduced under 1200 psi H₂, for 4-24 hrs, condition: at 140° C.and 200° C. LHSV = 1

As comparative examples, regeneration attempts that washed the catalystbed with water and/or bleach at 70° C. for up to 24 hours were noteffective. Catalyst activity exhibits no significant recovery orimprovement as compared to before regeneration.

FIG. 4 shows the relative concentration of sulfur (ppm) present on asponge-metal (Ni) fixed-bed catalyst over time. At the beginning, thesulfur concentration is significant in the reactor (˜8.800-8.900 ppm),but the nickel bed soon reduces the sulfur concentration to less thanabout 400 ppm or 500 ppm. This level is maintained after eachregenerative treatment with hot water solution. These results suggestthat sulfur poisoning can be effectively controlled and reduced.

FIG. 5 presents the effect of regenerating a Raney nickel fixed-bedcatalyst with subcritical hot water (170° C.), as expressed in terms ofthe relative percent efficiency of converting a sugar feedstock inhydrogenation reactions. Starting with a fresh catalyst, a firsthydrogenation reaction runs for about 140 hours, after which thecatalyst is washed. The first reaction run operated at near 100%efficiency converting sugar (i.e., ˜97% or 98%). After the first washwith deionized subcritical water, the reaction exhibited similar orslightly better efficiency. A second reaction ran for about 95 hours,and exhibited a lower conversion rate (˜85%-88%), which was increased toabout 95% efficiency after a second regenerative wash. In a thirdreaction, run for about 96 hours, the efficiency rate had decreased toabout 70%, which was increased slightly after a third regenerative wash;but increased to about 94% or 95% after a fourth and fifth washes. Theseresults seem to suggest that the wash treatment temperature appliedand/or duration of later washes may need to increase for laterregenerative attempts.

FIG. 6 summarizes relative efficiency of sugar conversation in ahydrogenation reaction over about an extended period during whichsponge-metal catalysts were subjected to regenerative treatment with ahot water solution according to the present invention when the catalyticefficiency seemed to flag. As one can see, sugar conversion rates weremaintained at relatively high levels of about 94% or 95% or greater,like in FIG. 5. After each regenerative wash, sugar conversion increasedfrom about 95% to about 98% with the same feed.

FIG. 7 shows that the amount of unreacted sugar that remains in a finalproduct of the hydrogenation reaction can be significantly reduced. Atthe beginning of the hydrogenation reaction run, the amount of sugarconcentration in the product is low, indicating that the catalyst isoperating at high efficiency. Over the course of hydrogenation, theamount of unreacted sugar remaining in the product increases. At about400 hours into the reaction run, the sugar concentration is at about8.000-10.000 ppm: later at about 500 to 600 hours sugar levels havereach about 24,000-28,000 ppm, which for some commercial uses isunacceptable.

Normally, when residual sugar levels reach sufficiently highconcentrations, manufacturers will need to stop production and replaceor modify the catalyst at this point. Stopping production and removingor regenerating the catalyst, however, tends to be costly andeconomically inefficient. Hence, the present in situ regenerativetreatment and reactor system can help overcome such a problem, byproviding a parallel reactor configuration that can make productioncontinuous and eliminate the need to change catalysts after a relativelyshort production run.

After a regenerative treatment of the catalyst in the reactor, the graphin FIG. 7 shows that catalytic activity is restored, as evidenced by areturn to relatively low sugar concentration remaining in product evenafter prolonged hydrogenation run times of about 700-900 hours. Thecatalyst is washed and rinsed with subcritical water and/or a saltsolution (i.e., Ru/C) or a peroxide solution (i.e. Ni), according to aversion of the present invention. The agglomerated species on thecatalyst are removed. An interested phenomenon is that after thecatalyst is subject to the regenerative wash, the concentration of sugarthat remains in final product did not return to the initial highconcentrations but remained at a moderate level.

B

All fixed-bed catalytic reactions described in the following exampleswere performed in 30 cubic centimeter (cc) fixed bed reactors. Thereactor bodies are stainless steel with an internal diameter (ID) of0.61 inches. The reactors are jacketed and are heated with circulatingoil. Reactor temperatures are monitored via an internal thermowell ⅛″with a 1/16″ thermocouple that can slide up and down to monitor peaktemperature. The temperature of the jacket is monitored by measuring theoil temperature just before it enters the jacket. The temperatures ofthe reactors are controlled by adjusting the oil temperature. The inletsof the reactors are attached to an Isco dual piston pump and mass flowcontrollers for supplying gases. The outlet was attached to a condenserkept at 5° C. by a chiller unit. The pressures of the reactors arecontrolled using a dome loaded back pressure regulator (Mity Mitebrand).

In general the experimental conditions employed for the examples are:

Reactor jacket temperature: 140° C.-200° C.

Oil bath temperature: 90° C.

Reaction temperature: 80° C.

NaCl concentration: 40% by wt., total volume: 70 ml

Catalyst weight (wet): 20-25 g.

Sugar concentration: 30%-40% by wt.

Feed pH: 4.5-5.0

Hydrogen flow rate: 400 mL/min.

Pressure (H2) 1200 psi

Reaction time: 4 hrs.

Example 1

Used Ru/C catalyst from a vertical trickle-bed reactor is subjected toregeneration. About 85% catalytic activity remained of the catalystsample after about 16 hours of undergoing a hydrogenation reaction.Using about 70 mL of 40% NaCl solution was added to 25 grams of usedRu/C catalyst from both a top section and a bottom section of thereactor in 250 mL beaker, and the mixture was stirred for 4 hours at 70°C. The liquid was poured out and solid was added 100 ml DI water, andstirred for another 16 hours at 70° C. The solid catalyst was washed andrinsed with DI water five (5) times to removal any extra residual salt.The oligomer deposits on the catalyst surface are nearly completelyremoved, and catalytic activity recovered to about 93% or 95% ofprevious level for fresh catalyst.

Example 2

Similar to the conditions described in the example above, Ru/C catalystwas washed by hot water at 190° C. for 16 hours at 1200 psi, and thenwashed with 0.5% H₃PO₄ at 170° C. for 16 hours. This resulted inrecovery of about 90%-95% of former catalytic activity.

Example 3

In another regenerative example, after 240 hours of use in hydrogenationreaction, Ru/C catalyst is washed with hot water for 16 hours at 180° C.The catalyst activity was tested and found that the catalyst was able toconvert 99% of the sugar feedstock to sugar alcohols.

Example 4

Deactivated Ru/C catalysts (Sugar conversion, 85%) were loaded in a 30cc reactor, DI water was introduced to reactor by HPLC pump at rate of 1mL/min. The reactor was heated by outside oil jacket to 250° C. Thecatalyst was washed under high temperature for 16 hours, then cooleddown to room temperature. Catalytic activity was restored to be nearfull recovery, ˜98%.

Example 5

Sponge nickel fixed-bed catalysts are employed for sulfur removal. A 30%dextrose solution was used as feed to check catalyst activity at LHSV=1,140° C., 1200 psi H₂. After running hydrogenation reaction for 800-900hours with, the catalyst activity dropped to about 70% and 75% sugarconversion, respectively and 95% sulfur absorbance (7 ppm to 1 ppm).After hydrogenation reaction, the catalyst was washed with subcriticalwater for 18 hours at 150° C. Catalytic activity is restored: sugarconversion recovered to about 94-96%.

Example 6

Using a sponge-metal (Raney nickel) fixed-bed catalyst, carbohydratehydrogenation reaction was run in a 30 cc reactor at a H₂ pressure of1200 psi, at a reaction flow rate of 2 mL/min. for more than 340 hoursusing different feedstocks (pH 5.5.30% DS (8-10% DP)), which containedabout 8 ppm to 12 ppm sulfur. The fix-bed was washed with subcriticalhot water (170° C.) for about 4 hours to remove adsorbed sulfurcompounds and regenerated the surfaces of the catalyst. After washing,the same feedstock was put into this reactor to test for relativeefficiency of sugar conversion after the sulfur removal. The results aresummarized in accompanying FIG. 5, discussed above.

The present invention has been described in general and in detail by wayof examples. Persons of skill in the art understand that the inventionis not limited necessarily to the embodiments specifically disclosed,but that modifications and variations may be made without departing fromthe scope of the invention as defined by the following claims or theirequivalents, including other equivalent components presently known, orto be developed, which may be used within the scope of the presentinvention. Therefore, unless changes otherwise depart from the scope ofthe invention, the changes should be construed as being included herein.

I claim:
 1. A continuous hydrogenation process, the process comprising:introducing a carbohydrate or sugar solution feedstock and hydrogen intoa reactor having a catalyst therein; reacting said feedstock in anaqueous solution under pressure; removing a resulting aqueous reactionproduct mixture, wherein said carbohydrate or sugar solution feedstockis introduced and reacted, and reaction product is removed in acontinuous manner; and periodically introducing a subcritical deionizedwater rinse into said reactor when catalytic activity of said catalystdecreases to a predetermined level as a consequence of sulfur orsulfuric contamination.
 2. The continuous hydrogenation processaccording to claim 1, wherein said reactor and catalyst are rinsed withsubcritical deionized water at a temperature between about 130° C.-250°C. for a period of between 4-48 hours.
 3. The continuous hydrogenationprocess according to claim 1, wherein said reactor system is configuredas with a first reactor section and second reactor section, eachinvolving a different kind of catalyst material, such that a first partreaction involves a first catalyst material and a second part reactioninvolves a second catalyst material.
 4. The continuous hydrogenationprocess according to claim 3, wherein said first and second reactorsections are arranged either in serial communication or in parallelcommunication relative to each other.
 5. The continuous hydrogenationprocess according to claim 4, wherein said first reactor section is usedalternatively with said second reactor section when in parallelcommunication, such that a reactor chamber is washable with saidsubcritical deionized water rinse at a given time, without interruptionof said hydrogenation process.
 6. The continuous hydrogenation processaccording to claim 1, further comprising introducing a deionized aqueoussolution containing H₂O₂ in a concentration of ≦7% by volume to saidfirst catalyst in said first reactor when catalytic activity of saidfirst catalyst decreases to a predetermined level.
 7. The continuoushydrogenation process according to claim 3, further comprisingintroducing periodically an aqueous salt solution to either first orsaid second catalyst in said reactor system, after reacting and removingsaid sugar solution feedstock and before introducing said subcriticaldeionized water rinse.
 8. The continuous hydrogenation process accordingto claim 3, wherein a metal of said first catalyst is Ni, or of saidsecond catalyst is selected from Ru, Pt, and Pd.
 9. The continuoushydrogenation process according to claim 3, wherein said first partreaction removes sulfur and/or sulfides from said feedstock, beforereacting in said second part reaction.
 10. The continuous hydrogenationprocess according to claim 3, wherein either said first catalyst orsecond catalyst exhibits regenerated catalytic activity after washingwith said subcritical deionized water rinse, and prolonged catalyticactive duration of at least two to three (2×-3×) times longer than thatof a catalyst that is not washed with said subcritical deionized waterrinse.